CA2801228A1

CA2801228A1 - Method and apparatus for the purification of carbon dioxide using liquide carbon dioxide

Info

Publication number: CA2801228A1
Application number: CA2801228A
Authority: CA
Inventors: Rasmus Find
Original assignee: Union Engineering AS
Current assignee: Union Engineering AS
Priority date: 2010-06-17
Filing date: 2010-06-17
Publication date: 2011-12-22
Also published as: US20130152628A1; AU2010355553A1; CN102946972B; DK2582445T3; AR081924A1; US11287183B2; JP2013534504A; EP2582445B1; MX2012013106A; MY159234A; KR101663670B1; AU2010355553B2; BR112012031705A2; KR20130114069A; US20170227285A1; NZ605796A; EP2582445A1; ZA201208786B; JP5795366B2; EA201291434A1

Abstract

The present invention relates to an improved method for removing contaminants from a gaseous or liquid stream substantially comprising carbon dioxide. More specifically, the method comprises the step of subjecting the gaseous or liquide stream to an absorption step in which the absorbent is liquid carbon dioxide or a rectification step wherein the waste of carbon dioxide is minimized by utilizing a compressing means for generating a pressure difference between two streams in a reboiler.

Description

METHOD AND APPARATUS FOR THE PURIFICATION OF CARBON DIOXIDE USING LIQUIDE
CARBON DIOXIDE

The present invention relates to an improved method for remov-ing contaminants from a stream substantially comprising carbon dioxide.
More specifically, the method comprises the step of subjecting the stream to a purification step in which liquid carbon dioxide is used and wherein the waste of carbon dioxide is minimized by generating a pres-sure difference between two streams in a reboiler.

Background of the Invention Carbon dioxide recovery plants are widely used to clean and/or recover carbon dioxide released e.g. from combustion of hydrocarbons, fermentation and gas processing.
When producing food grade carbon dioxide or carbon dioxide for other applications, where a high purity is required, contaminants must be removed in up and/or down stream equipment in order to obtain the required purity. Conventional technologies available for removing such contaminants include for example scrubbing, oxidation, adsorption and/or distillation. Also, the introduction of a flash column step between an absorber and a stripper has been reported e.g. in WO 2007/009461 in which NO2 is removed in a flash column located between an amine ab-sorber and a stripper. NO2 is difficult to separate further down stream in the purification process where the carbon dioxide is in liquid form, since NO2 is almost irreversibly dissolved therein.
Another purification step is water scrubbing; in a water scrubber all water-soluble contaminants are removed from the gaseous source.
The drawbacks of using a water scrubber is the large amounts of clean water used and wastewater formed.
Another purification step for a carbon dioxide containing gas is dehydration. In a dehydration step any water present in the gas is ab-sorbed and thereby removed from the gaseous stream. Also, if any resi-dues of acetaldehyde, volatiles and/or oxygenates are present in the gas, some of these compounds are also removed in a desiccant, depend-ing on the dehydrator used.

However, if the gas comprises impurities, which are heavily dis-solved in carbon dioxide, i.e. primarily non-polar organic compounds and compounds having a boiling point higher than the boiling point of carbon dioxide under the prevailing conditions, these will not be effectively re-moved from the stream using a water scrubber. For these compounds an adsorption filter, e.g. activated carbon, must be used.
This problem has been addressed in PCT/DK2009/050159 where pure liquid carbon dioxide is used to remove the above-mentioned impu-rities. This method has the drawback that when most of the impurities have a boiling point above the boiling point of carbon dioxide at the pre-vailing conditions, the amount of pure liquid carbon dioxide has to be in-creased in order to remove all impurities effectively. Increasing the ab-sorbent liquid carbon dioxide, results in a huge loss of product carbon dioxide, which makes the method uneconomical.
Thus, as the yield of carbon dioxide is very important, measures must be taken in order to recover the carbon dioxide. In the prior art the contaminant rich liquid carbon dioxide that would otherwise be wasted was reboiled and fed to the feed stream again for purification. However, such prior art measures requires large amount of energy to be supplied to the process, which renders the process less economic, and in particu-lar for streams substantially comprising contaminants having a boiling point above the boiling point of carbon dioxide. In addition, the energy consumption increases with increasing amounts of liquid carbon dioxide used, therefore one of the objects of the prior art was to keep the liquid carbon dioxide and energy consumption at a minimum without compro-mising the quality of the recovered carbon dioxide The object of the present invention is to provide a method and plant in which all of the above problems have been solved in an im-proved.
Summary of the Invention In one aspect, the present invention relates to a method for re-moving at least one contaminant from a gaseous feed stream substan-tially comprising carbon dioxide, said method comprising the step of subjecting the feed stream to a purification step under conditions provid-ing a carbon dioxide enriched gaseous stream and a contaminant rich liquid stream.
This problem is in its broadest sense solved by purifying a feed stream in a purification column providing at least a contaminant rich liq-uid stream and a contaminant lean gaseous stream and reboiling the contaminant rich liquid stream providing a gaseous stream and feeding the gaseous stream to the purification column, wherein a pressure dif-ference between the contaminant rich liquid stream and the contaminant lean gaseous stream is provided before the streams enter the reboiler wherein Pcontaminant rich liquid stream < Pcontaminant lean gaseous stream=
The above mentioned problems are in a more specific embodi-ment solved by a method comprising the step of subjecting a feed stream (f) to a) a purification step in a column having a top, bottom and an intermediate section, the purification step provides a contaminant lean gaseous stream (g2) leaving the top section of the column and a con-taminant rich liquid stream (12) leaving, optionally the bottom section of, the column and wherein the contaminant lean gaseous stream (g2) leav-ing the top section of the column is further subjected to the steps se-lected from:
1:
b1) compressing the contaminant lean gaseous stream (g2) providing a compressed gaseous stream (g4);
c1) cooling the compressed gaseous stream (g4) in a reboiler providing at least a product stream (p) and a gaseous stream (g3); and d1) feeding the gaseous stream (g3) to the purification column at the bottom section of the column;
or 2:
b2) cooling the contaminant lean gaseous stream (g2) in a re-boiler providing at least a product stream (p) and a gaseous stream (g3); and c2) compressing the gaseous stream (g3) providing a cooled compressed gaseous stream (g4');
d2) feeding the cooled compressed gaseous stream (g4') to the column at the bottom section of the column; and depressurising the contaminant rich liquid stream (12) leaving at the bottom section of the column before entering the reboiler.
The depressurisation is in a particular embodiment obtained by means of a valve.
The present inventors have found that by circulating the con-taminant lean carbon dioxide stream and compressing and utilizing the energy for re-evaporating the contaminant rich liquid carbon dioxide in the reboiler, very large amounts of liquid carbon dioxide can be reboiled without the consumption of large amounts of externally supplied energy.
This is due to the fact that when the pressure is increased by 1 bar - the corresponding saturation temperature of carbon dioxide will in-crease approximately 3 K ( C) and vice versa. In this way a temperature difference can be obtained allowing a heat exchange between hot and cold streams. Thus, what the inventors have realized is that by the solu-tion of the invention a sufficient temperature differences can be obtained between the two streams for recovering carbon dioxide from the con-taminant rich stream in a more economical way than by using an exter-nal heat source in the reboiler.
The present invention has several advantages. By increasing the amount of liquid carbon dioxide used as absorbent, the feed stream will be recovered at a much higher degree of purity. By the solution provided the increasing amount of liquid carbon dioxide used does not compro-mise the overall economy of the method, i.e. the yield and energy con-sumption.
The prior art method according to PCT/DK2009/050159, in which the object was to minimize the amount of carbon dioxide in the waste stream, showed that after a certain amount of absorbent liquid carbon dioxide (above 400 kg/hour) washing out of contaminants oc-curred. When increasing the amount of absorbent liquid carbon dioxide, more and more amounts and types of contaminants were washed out in a non-linear manner - meaning that no linear relationship exists be-tween the volume of absorbent used and the degree of purification ob-tained.
However, the amount of wasted carbon dioxide also increases 5 dramatically resulting in huge amounts of carbon dioxide to be reboiled and purified again (see the comparative example). Though this results in pure carbon dioxide the over all process becomes uneconomical because of either the high waste of carbon dioxide or the large amount of energy that must be supplied to the reboiler, and the subsequent cooling of the product stream, in order to recover the liquid carbon dioxide comprising contaminants.
In the reboiler the present invention utilizes the differences in pressure between the liquid stream entering the reboiler (i.e. 12) and the gas entering the reboiler (i.e. g2 or g4, depending on the embodiment).
This difference in pressure is provided by the compressing means or the compressing means and the valve.
In its broadest sense the effect can be obtained by two alterna-tives either by (1) inserting the compression step on the contaminant lean gaseous stream, or (2) inserting the compression step on the gase-ous stream effluent from the reboiler combined with a depressurisation step before the contaminant rich liquid enters the reboiler. The depres-surisation is in this embodiment preferably performed by inserting a valve.
The liquid before the valve has a pressure pl which is higher than the pressure p2 of the liquid having passed the valve. Similarly ap-plies to the gas entering the compressor where the gas entering the compressor has the pressure p2 and the gas leaving the compressor has the pressure pi, which is higher. The difference in pressure, whether the stream is liquid or gaseous, is the same.
Providing for this difference in pressure on these specific streams of the process has the important effect of changing the dew point and bubble point of the streams. This effect renders very high lev-els of absorbent liquid dioxide relative to feed stream economical. In fact using this method any amount of absorbent liquid carbon dioxide can be used without rendering the process uneconomical.
Thus, the energy contained in the purified gaseous carbon diox-ide stream is utilized to recover otherwise wasted carbon dioxide with only little supply of external energy.
The feed stream may be both liquid and gaseous. When the feed stream is liquid, the method preferably comprises the steps b1) compressing the contaminant lean stream (g2) providing a compressed gaseous stream (g4); c1) cooling the compressed gaseous stream (g4) in a reboiler providing at least a product stream (p) and a gaseous stream (g3); and d1) feeding the gaseous stream (g3) to the column at the bottom section of the column (alternative 1).
When the feed stream is gaseous both embodiments are advan-tageous, however particularly preferred is the method comprising the steps b2) cooling the contaminant lean stream (g2) in a reboiler provid-ing at least a product stream (p) and a gaseous stream (g3); and c2) compressing the gaseous stream (g3) providing a cooled compressed gaseous stream (g4'); d2) feeding the cooled compressed gaseous stream (g4') to the column at the bottom section of the column; and de-pressurising the contaminant rich liquid stream (12) leaving at the bot-tom section of the column before entering the reboiler (alternative 2).
When the compressor is placed after the reboiler, the duty re-quired is smaller as compared to the duty required in alternative 1;
therefore a smaller compressing means can be used. Moreover, it is pos-sible to use, e.g. an oil lubricated compressor, which is a less costly al-ternative. Trace amounts of oil in the gaseous stream caused by this compressor is immediately removed in the purification column. Thus, this alternative saves cost on both construction of the plant and the sub-sequent operation.
Depending on the nature of the feed stream the purification step will either be an absorption or a rectification process. Thus, when the feeding stream is liquid the purification step is a rectification and when the feeding stream is gaseous the purification step is an absorption process.
In a particular embodiment where the feed stream (f) is essen-tially liquid the compression step d) is performed according to alterna-tive 1. When the feed stream is liquid the embodiment of alternative 2 will be less efficient, as the contaminant rich liquid stream (12) leaving the bottom section of the column will be very low consequently the pres-sure difference provided by the valve on that stream will have a minimal effect.
However, when the feed stream (f) is gaseous the compression step d) can be equally performed according alternative 1 and 2, however in an even more preferred embodiment according to alternative 2. This is due to the lower cost of construction and the reduced amount of en-ergy used to compress the smaller volume of the gaseous stream (g3) as compared to the contaminant lean gaseous stream (g2).
The pressure in the column is normally between 10 and 40 bar, however, other pressures are contemplated, for example if the tempera-ture of the liquid absorbent carbon dioxide is higher than the freezing temperature of water and hydrates, such as gas and liquid hydrates, un-der the prevailing pressure, the carbon dioxide would also be able to remove water from the stream.
Under the above pressure conditions, a preferred temperature range of the gaseous feed stream is 5 to 25 C, more preferred 5 to 15 C, such as 10 C, although temperatures in the range of -40 to 40 C
are contemplated if operating at another pressure.
The dew point temperature of carbon dioxide in the above men-tioned pressure range is -40 to +5.5 C; it is within the skill of the art to determine the dew point temperature of carbon dioxide at any given pressure.
The method of the present invention is particularly useful for removing contaminants having a boiling point higher than the boiling point of carbon dioxide at the prevailing conditions and/or non-polar compounds. These compounds are not effectively removed by other high through put methods. Such compounds may be but are not restricted to sulfides, such as hydrogen sulfide, carbonyl sulfides and dimethylsulfide;
nitrogen containing compounds, such as N2, ammonia and nitrogen diox-ide; and hydrocarbons, such as, methane, n-pentane, n-hexane, ben-zene, toluene and oxygen containing hydrocarbons such as dimethyl ether, acetaldehyde, ethyl acetate, acetone, methanol, ethanol, isobu-tanol and n-propanol. The method provides a carbon dioxide enriched gaseous stream and a contaminant enriched liquid stream comprising at least 95 % (w/w) of each of the at least one contaminant(s) specified above as compared to the content in the feed stream.
In a particular embodiment, the absorbent liquid carbon dioxide is an externally supplied source of liquid carbon dioxide, particularly pre-ferred partially a stream from the down stream carbon dioxide purifica-tion process. The carbon dioxide stream may in this embodiment be dis-tilled liquid carbon dioxide or condensed carbon dioxide.
The advantage of this embodiment is that the absorbent, which is used in the column, has a high purity; consequently, there will be no accumulation of impurities in the gaseous phase above the purification column. Moreover, the carbon dioxide of higher purity will have im-proved absorbing properties. This is particularly advantageous in facili-ties where a potential build up of contaminants occur frequently, even when contaminants are present in smaller amounts. An external sup-plemental supply of absorbent liquid carbon dioxide is often necessary in the present invention when the volume of absorbent liquid carbon diox-ide by far exceeds the volume of the feed stream.
Also, when operating at very high absorbent rates, e.g. higher than the actual capacity rate of the plant, externally supplied carbon di-oxide may be necessary.
In a presently preferred embodiment the ratio of absorbent liq-uid carbon dioxide to feed stream is 1:3 to 10:1, preferably 1:3 to 3:1 such as 1:2, 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1 and 9:1. Depending on the impurity profile the ratio may be in the lower end, such as a ratio of 1:1 to 5:1 also provided in PCT/DK2009/050159.
In another embodiment is provided a method for removing the at least one contaminant from the feed stream wherein the purification step comprises an integrated dehydration step, i.e. an integrated chemi-cal or physical drying step, respectively.
In the dehydration integrated embodiment, the feed stream comprising water is contacted with an agent capable of decreasing the water activity (a water inhibitor, a dehydrating agent), herein after "the water inhibitor". Such a water inhibitor is preferably fed in the purifica-tion column at a location between the mid section of the purification col-umn and above the inlet of the feed stream, when the feed stream is gaseous; in this context mid-section should be understood as being "mid" relative to the height of the column, i.e. the centre part of the in-termediate section. As mentioned, the temperature at the bottom of the column will be adjusted so that water does not freeze under the prevail-ing conditions. However, once being mixed with the water inhibitor, the freezing point of water is significantly reduced why the temperature is no longer as critical. Alternatively the water inhibitor may be fed at the same position as the feed stream or together with the feed stream, de-pending on the temperature of the feed stream.
The term water inhibitor contemplates any agent capable of de-creasing the water activity/inhibit water and may be selected from the group consisting of methanol, ethanol, mono ethylene glycol and tri eth-ylene glycol. Methanol and ethanol are particularly preferred. Due to the low temperature in the purification column, it is desired to select a water inhibitor that has a low viscosity under the prevailing conditions. Fur-thermore, it is desired to choose water inhibitors that are relatively inex-pensive and easy to recover; recovery of the water inhibitor, e.g.
methanol and ethanol is within the skill of the art. Ethanol may be pre-ferred, if the process is implemented in a bio-ethanol plant or a similar plant in which fermentation takes place i.e. where the water inhibitor, ethanol, is present in the facility so that no external supply of water in-hibitor is needed; thus, the water inhibitor is in a particular preferred embodiment bio-ethanol.
In particular the feed stream may comprise ethanol when origi-nating from a bio-ethanol production plant or a fermentation process. In this embodiment the feed stream may comprise sufficient ethanol to de-hydrate the feed stream in the purification column alternatively; addi-tional ethanol/water inhibitor may be added.
In yet another embodiment the water is removed by means of a water scavenger, such as ammonia.
When having an integrated dehydration step saving of space is even more improved as an upstream-located dehydration step, often employed, may now be omitted. In addition, the dehydration is more 5 flexible as the flow of inhibitor may be adjusted depending on the con-tent of water in a stream to be purified.
The absorbed water and water inhibitor/scavenger is preferably drawn from the purification column at the bottom section of the column along with the contaminant rich liquid stream.

10 In this embodiment, the contaminant rich liquid stream may also leave the column at a point higher than/above the inlet of the water inhibitor/scavenger into the column, e.g. between the water inhibi-tor/scavenger inlet and the mid-section of the column, in order to obtain a water inhibitor/scavenger lean carbon dioxide fraction that may be re-turned to the purification column after an evaporation step, e.g. in the reboiler.
In yet another embodiment a fraction of the contaminant rich liquid stream comprising the water inhibitor/scavenger and absorbed impurities is circulated in a loop. In this embodiment the contaminant rich liquid stream leaving at the bottom section of the purification col-umn is split in two so that a first contaminant rich liquid fraction of the liquid stream (12a) is recirculated to the inlet of pure water inhibi-tor/scavenger and mixed therewith. This saves consumption of water in-hibitor/scavenger in the over all process by exploiting the full ability of the water inhibitor/scavenger to bind water.
In a typical process according to the present invention, the wa-ter content is relatively low as compared to the capability of any of the above mentioned water inhibitors/scavengers to absorb water; therefore looping the water inhibitor/scavenger so that the water in the feed stream is inhibited by the water inhibitor/scavenger mixed with water, carbon dioxide and impurities as defined in the context of the present invention, will not impair the water inhibiting ability. Rather the ability of the water inhibitor/scavenger to bind water is fully exploited.
It is also contemplated that all of the above embodiments may be combined, i.e. that both an intermediate outlet for liquid carbon diox-ide in the upper part of the purification column, and/or a loop of waste liquid and/or a split loop of waste liquid may be present.
If the feeding gas comprises 02, NO and NO2, NO2 could also be absorbed in the liquid CO2. This would force the gas phase equilibrium 1/202 + NO <-> NO2 to the right. Consequently, substantial amounts of the NOx's would be removed from the stream as NO2 in the liquid CO2 leaving at the bottom of the purification column. As mentioned, NO2 fa-vours liquid carbon dioxide; once substantially pure liquid carbon dioxide is obtained NO2 is very difficult to separate off. By introducing the car-bon dioxide scrubber/rectifier, i.e. the purification column, gaseous streams comprising trace amounts of NOx's are additionally removed there from.
As the methods of the present invention is to be performed in an operating unit located within a larger unit, the methods are in a par-ticular embodiment followed by processing the product gaseous carbon dioxide leaving the column and reboiler by optionally heat exchange, op-tionally filtration, such as using an activated carbon filter, and finally dis-tillation, e.g. flash distillation or condensation, in order to give a pure liquid carbon dioxide product to be stored and sold. It is also contem-plated that the method of the invention is performed in two or more consecutive purification steps, such as 2, 3 or 4. Consequently, it is also contemplated that more than one purification unit of the invention are interconnected.
The method of the present invention also contemplates the product carbon dioxide directly obtained after purification using the claimed methods.
Likewise it is contemplated that upstream purification steps may be present, such as a condensation step in which a carbon dioxide rich gas and liquid is obtained followed by the absorption step according to the present invention.
In yet another aspect the present invention provides a carbon dioxide purification unit. This unit is particularly useful for operating the method of the present invention.

Thus, in the second aspect is provided a carbon dioxide purifica-tion unit comprising a purification column (Al) having a top and a bot-tom and a section intermediate of the top and the bottom, the purifica-tion column having a feeding stream influent (f), a contaminant lean gas purification column effluent (g2) situated at the top part of the column, a liquid carbon dioxide influent (11) situated at the top part of the column, and a contaminant rich liquid column effluent (12) situated at the bottom part of the purification column, wherein the contaminant rich liquid effluent (12) is connected to a reboiler (A3) additionally having a waste liquid effluent (13), a product effluent (p), a compressed gaseous influent (g4), and a gas effluent (g3), the gaseous effluent (g3) being connected to the purification col-umn (Al), wherein a compressing means (A2) is inserted between the reboiler (A3) and the purification column (Al) at a position between the contaminant lean gaseous purification column effluent (g2) and the compressed gaseous influent (g4); or wherein the contaminant rich liquid effluent (12) is connected to a reboiler (A3) additionally having a waste liquid effluent (13), a product effluent (p), a contaminant lean gas purification column effluent (g2), and a gas effluent (g3), the gas effluent (g3) being connected to a com-pressing means (A2) inserted between the reboiler (A3) and the purifica-tion column (Al) at a position between the gas effluent (g3) and a cooled compressed gaseous influent (g4') and wherein a valve (A4) is positioned between the contaminant rich liquid effluent and the reboiler (A3).
The purification column may be an absorption or rectification column known in the art, which is suitable for the particular purpose.
The nature of the purification column depends on whether the feeding gas is liquid or gaseous. When the feeding stream is gaseous the process in the purification column is an absorption process and when the feeding stream is liquid the process in the purification column is a rectification.
Size and dimensions vary depending on the size of the carbon dioxide purification plant. The choice of purification column is within the skill of the art. Pipes, pumps, valves etc. are also included and the spe-cific choice of and location of such additional elements is within the skill of the art. The intermediate section may be a packed section or if a tray type column, trays.
In one embodiment the feeding influent is situated at the top section of the purification column. In this embodiment the feeding stream is liquid and the contaminant rich liquid effluent is connected to a reboiler additionally having a waste liquid effluent, a product effluent, a contaminant lean gas influent, and a gas effluent, the gas effluent being connected to the purification column, wherein a compressing means is inserted between the reboiler and the purification column at a position between the cooled compressed gas purification column effluent and the contaminant lean gaseous influent.
When the feeding stream is gaseous the feeding influent is situ-ated at the bottom section of the purification column. The position of the reboiler and compressor can be both alternatives provided by the inven-tion.
In a particular embodiment, the contaminant rich liquid effluent (12) situated at the bottom of the column is split in two at a position out-side the column and a first contaminant rich liquid effluent (12') is fed to a water inhibitor and/or scavenger influent (10), and a second contami-nant rich liquid effluent (12") is disposed.
This set-up provides for recycling of the water inhibitor and/or scavenger. The branching of the pipe allows the stream to proceed in two ways. A valve may control the flows in either direction.
In another particular embodiment, the purification column is further provided with a carbon dioxide effluent (15) situated at a position between the water inhibitor and/or scavenger influent (10) and the liquid carbon dioxide influent (11).
If an effluent is positioned above the inlet where the water in-hibitor and/or scavenger is fed to the purification column, liquid carbon dioxide, essentially without water inhibitor and/or scavenger may exit the column for further purification, e.g. being recycled to the purification column.
In yet another embodiment, in which the purification unit is connected to the respective up and downstream operating units the feeding gas influent (g1) is connected to a feeding gas source, prefera-bly partially purified carbon dioxide; and/or the product effluent (p) is connected to a carbon dioxide processing unit, such as a heat exchanger and/or a filter and/or a distillation column; and/or the liquid carbon diox-ide influent (11) is connected to a liquid carbon dioxide reservoir, e.g. the distillation column connected to the product effluent; and/or the waste liquid effluent (13) is connected to a waste reservoir and/or the water in-hibitor and/or scavenger influent; and/or the water inhibitor and/or scavenger liquid influent (10) is connected to a water inhibitor and/or scavenger reservoir.
In still another embodiment, the carbon dioxide effluent (15) is connected to a carbon dioxide purification unit, such as the purification column (Al). This embodiment reduces the amount of liquid carbon di-oxide that may be mixed with the water inhibitor and/or scavenger. As it may be difficult to remove the water inhibitor and/or scavenger from the waste liquid stream, this will be of importance if substantial amounts of carbon dioxide are present in the waste liquid.

Figures Figure 1 is a flow chart embodying the method of the invention where the compression step/means is positioned according to alternative 1.
Figure 2 is a flow chart embodying the method of the invention where the compression step/means is positioned according to alternative 2.
Figure 3 is a schematic illustration of a presently preferred em-bodiment of alternative 1 of the carbon dioxide purification unit of the present invention in which dehydration of the stream is integrated.
Detailed Description of the Invention According to the present invention, a substantially pure CO2 stream and/or feed stream comprises more than 80 weight-% CO2.
Throughout the description, unless otherwise indicated, all con-tents are given as weight-%.
Throughout the description and claims the reference numerals are the same when referring to a stream (for methods) and influ-ent/effluent (for purification units). Each stream assigned the same ref-5 erence will have the same prefix and then being denoted stream or in-fluent/effluent respectively depending on the context.
It is contemplated that all embodiments and variations of the method and purification unit apply equally to both said method and unit.
Thus, when referring to the method the suffix applied is 10 "stream" when referring to the purification unit the suffix "influ-ent/effluent" is applied. It is contemplated that streams/influents/-effluents having the same prefix correspond, this is further detailed be-low.
Streams and influents/effluents 15 Feed stream (f); Product stream (p); Contaminant lean gaseous stream (g2); Gaseous stream (g3); Second gaseous stream (g3a);
Compressed gaseous stream (g4); Cooled compressed gaseous stream (g4'); Filtered gas stream (g5); Non-condensable gases (g6); Water in-hibitor and/or scavenger stream (10); Liquid carbon dioxide stream (11);
Contaminant rich liquid stream (12); First contaminant rich liquid stream (12a); Second contaminant rich liquid stream (12"); Waste liquid stream (13); Second waste liquid stream (13a); Split second liquid stream (13b) Carbon dioxide stream (15); Condensed/distilled liquid carbon dioxide (16).
Components Purification column (Al); Compression means (A2); Reboiler (A3); Valve (A4); condenser (A5); Filter (A6); Condenser/distillation col-umn (A7); Pump (A8); Heat exchanger (A9).
Throughout the description and the claims the terms impurity and contaminant may be used interchangeably having the same mean-ing in the context of the present invention and both cover undesired substances in a carbon dioxide stream that should be removed.
Throughout the description and the claims the terms water ac-tivity reducing agent, agent and water inhibitor and/or scavenger may be used interchangeably having the same meaning in the context of the present invention, and all cover a substance that is capable of removing water from a carbon dioxide stream.
Throughout the description and the claims the term water free or dry gaseous stream is a gaseous stream in which the water content is so low so as not to cause process related problems, such as freezing within pipes, containers etc. More specifically a water free or dry gase-ous stream may be defined as a stream wherein the dew point tempera-ture of water under the prevailing process conditions is lower than the temperature of the stream.
The purification process described in greater details below typi-cally takes place in a traditional column of the absorber, scrubber or rec-tification type. The specific choice of column depends on the size of the facility, the nature of the feed stream and other factors; this is within the skill of the art.
All illustrations appended to the present description should be understood as a section of a larger facility. All features and variants of each of the embodiments and aspects described herein apply equally to all embodiments and aspects, i.e. both the method and the plant.
The method of the present invention can be applied in any car-bon dioxide recovery process at a point where the pressure of the feed gas is higher than the triple point pressure of carbon dioxide. Thus, pref-erably the method is used on a feed gas having a high carbon dioxide content.
The method can be applied to but is not limited to streams originating from a flue gas, a fermentation gas, petrochemical combus-tion gases and carbon dioxide from natural sources.
If the gaseous source is a flue gas the method of the present invention will typically be preceded by an amine absorption step option-ally followed by flash distillation, and stripping as described in EP 1 907 319 B1. Alternatively, the flue gas is condensed and subsequently ab-sorbed in a physical absorbing agent as described in EP 1804956 A.
In applications where the source gas is from a natural source, a fermentation process or a petrochemical process, the method of the pre-sent invention will typically be preceded by compression and optionally drying. The applications described above are examples and the invention should not be limited to these specific applications.
Detailed descriptions based of the drawings apply equally to the method and purification unit of the present invention.
Referring now to figure 1, an embodiment of the present inven-tion is illustrated in which a feed stream f may be liquid or gaseous, with the proviso that the inlet is situated at the top section of the purification column when the feed stream is liquid.
In figure 1 is shown a purification column Al, a compression means A2 and a reboiler A3.
The streams shown are the feed stream f, a liquid carbon diox-ide stream 11, a contaminant lean gas stream g2 leaving at the top of the purification column, a contaminant rich liquid stream 12 leaving at the bottom of the purification column, a compressed gaseous stream g4 leaving the compressing means, a gaseous stream g3 leaving the re-boiler, a waste liquid stream 13 leaving the reboiler, and a product stream p, leaving the reboiler.
The interaction of streams in the reboiler is as follows: The colder contaminant rich liquid stream 12 enters the reboiler in which it is heated by the warmer compressed gaseous stream g4. After the heat exchange, the contaminant rich liquid stream 12 turns into the gaseous stream g3 and the waste liquid stream 13 (i.e. the portion of 12 that is not re-evaporated). The warmer compressed gaseous stream g4 be-comes the product stream p, which may be liquid, gaseous or both.
Hence, 12 is the contaminant rich liquid carbon dioxide stream comprising the absorbed/washed/scrubbed out contaminants. The con-taminant rich stream 12 is fed to the reboiler A3 where it is reboiled pro-viding the gaseous stream g3 and the waste liquid 13, which is optionally discarded. The contaminant lean gaseous stream g2 is compressed by means of a compressor or blower providing the compressed gas g4, which is fed to the reboiler A3.
The product stream p may be both gaseous, liquid and a mix-ture depending on the conditions. The product stream may be further purified as desired for example by, but not limited to, heat exchanging and flash distillation and/or condensation to provide high purity liquid carbon dioxide to be stored in a tank or used directly. This high purity liquid dioxide directly obtained by any of the methods is also contem-plated.
Before entering the purification column Al, the feed stream f may be passed through a filter and/or a heat exchanger in order to con-dition the feed stream f for entering the purification column. The feed stream f may be both gaseous and/or liquid, thus the preconditioning depends on whether a gaseous and/or liquid feed stream is desired.
Normally, the feed stream is gaseous when the method of the invention is part of a complete carbon dioxide production plant. A liquid feed stream will most likely be relevant when non-pure carbon dioxide is supplied from an external source and is to be further purified according to the method of the present invention.
In one embodiment it may be desirable to prepare the feed stream f so that the temperature is well above the dew point tempera-ture of carbon dioxide at the given conditions. The pressure in the purifi-cation column will typically be around 6 to 25 bar in the food and bever-age industry, such as between 15 and 23 bar, e.g. 22.8 bar. In other applications, pressures are, however, also contemplated such as up to 60 bar, e.g. 40 to 55 bar, or even higher. The dew point temperature of carbon dioxide at 10 bar is -40 C; therefore, at that pressure the tem-perature of the stream entering the column should preferably be higher than this temperature.
When the appropriate pressure has been chosen it is within the skill of the art to choose the appropriate temperature of the feed stream.
When the temperature of the feed stream is well above the dew point of carbon dioxide when entering the column, the amount of liquid carbon dioxide in the bottom stream is minimized.
It is also contemplated that the gaseous feed stream is cooled, and optionally liquefied before entering the purification column; in this embodiment the contaminant rich liquid stream will comprise a higher amount of carbon dioxide than when the feed stream is gaseous.

The contaminant lean gaseous stream leaving the purification column is fed to a compressor in which the difference in pressure is pro-vided.
Referring now to figure 2 an embodiment of the present inven-tion is illustrated in which the influent feed stream shown is gaseous. In figure 2 the denotations are the same as given in figure 1 it is also con-templated that the feed stream is liquid and would consequently be situ-ated at the top section of the purification column.
In this embodiment the compressing means is situated after the reboiler so that the gaseous stream g3 is compressed before entering the purification column. In this embodiment a valve A4 is placed to de-pressurise the contaminant rich liquid stream 12 before entering the re-boiler, providing the necessary difference in pressure. In this embodi-ment the duty of the compressing means may be lower as compared to the first embodiment. This is due to the lower amount of carbon dioxide passing through in the gaseous stream g3 as compared to the contami-nant lean gaseous stream g2. Furthermore, a cheaper compressor may be used, e.g. an oil lubricated compressor, as the compressed gaseous stream provided, g4', is immediately purified removing any traces of oil from the stream.
Referring now to figure 3 an embodiment of the present inven-tion is illustrated in which the influent feed stream is gaseous. In figure 3 the denotations as given in figures 1 are the same.
Additionally, in figure 3 is shown a liquid stream 10 entering the purification column for example at a position above the feeding stream f and below the mid section of the column. The stream 10 comprises the water inhibitor and/or scavenger, e.g. methanol, ethanol, monoethyle-neglycol, triethylene-glycol or ammonia and is therefore a water inhibi-tor/scavenger feed stream. It is also contemplated that 10 is fed together with or at the same position as the feed stream f or is mixed with the feed stream f before entering the column.
When the feed stream originates from a bioethanol or fermenta-tion plant the stream may comprise ethanol and it may not be necessary to add additional water inhibitor to the purification column. Thus, in a particular embodiment the feed stream originates from a bioethanol plant or a fermentation process and the water inhibitor is fed together with the feed stream.
In principle the water inhibitor/scavenger may be fed at any po-5 sition of the column, however it is preferred that it is fed at the lower section of the column in order to minimize contamination of the con-taminant lean gaseous stream g2.
In the embodiment shown the contaminant rich liquid stream 12 leaves the column at a position above the inlets of the feed stream and 10 the water inhibitor/scavenger, respectively. In this embodiment the waste liquid stream 13 re-enters the column for use in the lower section, where it is used to scrub out impurities of the incoming gaseous streams fed to the lower part of the column Al.
In the embodiment shown a first contaminant rich liquid stream 15 12a is partly recirculated to the column, this recirculation may be omit-ted. Thus, at the bottom section of the column the first contaminant rich liquid stream 12a is withdrawn and at least a portion of the stream is fed to the purification column as a split liquid stream 13b. A second waste stream, 13a, is discarded. The split liquid stream 13b may optionally be 20 subjected to a heat exchanging step (not shown), providing, if heated, either a gaseous stream g3a or a gas liquid mixture or, if cooled, the split liquid stream further cooled. The provision of the recirculation pro-vides either a higher degree of purity when a liquid stream is provided, i.e. the heat exchanger cools, or a higher yield, when the heat ex-changer provides heat. This set up will result in a very pure product steam p and a very low degree of waste carbon dioxide (ultimately 13a) without using excessive water inhibitor/scavenger otherwise used if the increased contact between contaminant rich and contaminant lean fluids were to be conducted at the upper part of the purification column.
In the embodiment shown the product is further purified by fil-trating (A4), optionally through an activated carbon filter, liquefaction by means of a condenser (A5) and/or a distillation column (A5' - not shown) providing a condensed/distilled liquid carbon dioxide stream 16 and the stream of non-condensable gases g6.

It is also contemplated that liquid carbon dioxide may be with-drawn at a position above the inlet of the water inhibitor/scavenger and the contaminant rich liquid stream (12) outlet. This stream is denoted a carbon dioxide stream 15 (not shown). The advantage of this embodi-ment is that the water inhibitor/scavenger is not contaminated with an impurity from which the water inhibitor/scavenger cannot be recovered.
In this embodiment the contaminant rich liquid stream is preferably situ-ated at the lower part of the column.
In a further embodiment (not shown) the contaminant rich liq-uid stream 12 leaving the column is split into the streams 12a the first liquid stream and 12" a second liquid stream. 12" is fed to a second re-boiler and 12a is mixed with the water inhibitor/scavenger stream 10 and re-enters the column in a mixture as the water inhibitor/scavenger. 12a comprises carbon dioxide, contaminants, water and the water inhibi-tor/scavenger stream. This looping of the water inhibitor/scavenger is feasible despite the fact that pure inhibitor is mixed with the first liquid stream 12a because pure inhibitor will often have a water binding capac-ity which exceeds the amount of water present in the feed stream f.
Therefore, by looping the liquid stream 12a to the stream 10, both con-sumption of water inhibitor/scavenger and the volume of the first liquid stream 12a will be reduced, both resulting in overall savings. The ratio of the first liquid stream 12a that is mixed with the water inhibitor/scaven-ger stream 10 to the contaminant rich stream 12 depends on the water inhibitor/scavenger used. The skilled person will be able to determine the optimal ratio.
In this embodiment the second liquid stream 12" is fed to the reboiler A3 and re-evaporated and purified according to the invention.
It is, however, also contemplated by the present invention that the first liquid stream 12a is fed to the column again, optionally after be-ing re-evaporated, i.e. the stream 12a is not mixed with 10. This em-bodiment may be desirable if unexpectedly large amounts of water are present in the feed stream f, or if the stream 10 is diluted beforehand so that the concentration of water inhibitor/scavenger is low.
Another situation where 12a is not mixed with 10 could be if the first liquid stream (12a) comprises contaminants which react with the water inhibitor/scavenger creating undesired side-products.
The absorbent liquid carbon dioxide may be fully or partially originating from the gaseous feed stream to be purified. This embodi-ment is suitable when the amount of liquid carbon dioxide to be used is relatively low, such as 400-2000 kg/hour, alternatively it can be used as a supplement to externally supplied liquid carbon dioxide, and is particu-larly used when the feeding stream is gaseous. In this embodiment the purification column, in which the method is taking place, is provided with a condensing means, preferably in the top section of the column. When the, preferably gaseous, carbon dioxide feed stream contacts the con-densing means, a fraction of the gas will condense and, due to the higher density, run in the opposite direction than the gaseous stream and act as the absorbent/rectification liquid. This construction has sev-eral advantages; first of all, the set up is relatively simple and part of the absorbent originates from the feed stream to be purified.
The present invention will now be illustrated in more details by way of the following non-limiting example.

Comparative example Purification of gaseous carbon dioxide according to the method of the prior art at a constant pressure of 22.8 bar in the column, at a constant feeding gas temperature of 10.70 C and at a constant liquid carbon dioxide temperature of -18.20 C is illustrated in the table below with varying flow rates of the liquid absorbent carbon dioxide stream.
The number given in the column TB ( C) is the boiling point of each of the components at 1 bar(a). The loss of carbon dioxide indicated in the top row is loss without any provisions for recovery of the contaminant rich liquid stream (12).

Carbon dioxide loss (kg/hour) 1562.8 1066.1 817.9 718.6 619.4 173.8 74.9 2.9 Liquid CO2 fed to column (Kg/h) TB C
Flow rates (kmole/h) Feed gas % Recovery to waste liquid outlet Nitrogen 0.01 1.43 0.97 0.75 0.65 0.56 0.15 0.06 0.00 -195.8 Oxygen 0.01 2.68 1.83 1.41 1.23 1.06 0.30 0.13 0.01 -182.98 Methane 0.01 3.15 2.15 1.65 1.45 1.25 0.35 0.15 0.01 -161.49 Carbon Dioxide 100.00 24.41 18.07 14.47 12.95 11.36 3.47 1.53 0.06 -78.48 Hydrogen Sulfide 0.01 43.41 30.14 23.29 20.53 17.77 5.28 2.49 0.19 -60.35 Carbonyl Sulfide 0.01 95.43 86.96 77.41 71.93 65.30 21.36 9.52 0.32 -50.15 Dimethyl Ether 0.01 99.87 99.46 98.71 98.09 97.07 67.01 37.51 0.66 -24.84 n-Pentane 0.01 99.90 99.60 99.03 98.55 97.78 74.15 49.36 1.81 36.07 Nitrogen Dioxide 0.01 100.00 100.00 99.99 99.99 99.98 99.56 98.04 2.72 20.85 n-Hexane 0.01 100.00 100.00 99.99 99.99 99.98 99.61 98.52 5.01 68.73 Acetaldehyde 0.01 100.00 100.00 100.00 100.00 100.00 99.98 99.89 4.81 20.85 Ethyl Acetate 0.01 100.00 100.00 100.00 100.00 100.00 99.99 99.98 61.40 77.06 Dimethyl Sulfide 0.01 100.00 100.00 100.00 100.00 100.00 100.00 99.99 10.61 37.33 Benzene 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 60.87 80.09 Acetone 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 69.76 56.25 Toluene 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 99.40 110.63 Methanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 99.71 64.7 Ethanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 99.88 78.29 Isobutanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 99.99 107.66 n-Propanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 97.2 Feed gas temp C 10.70 Gas Outlet temp C -19.01 -19.01 -19.00 -19.01 -19.00 -18.97 -18.95 -17.68 Liquid Feed temp. C -18.20 Liquid outlet temp. C -18.83 -18.75 18.74 -18.75 -18.57 -17.66 -16.28 5.24 Liquid outlet flow of CO2.
kmole/hr 35.51 24.22 18.58 16.33 14.07 3.95 1.70 0.07 % CO2 loss of liquid inlets 78.14 71.07 65.43 62.49 58.99 28.96 14.97 0.74 % CO2 loss of total CO2 amountb 24.41 18.07 14.47 12.95 11.36 3.47 1.53 0.06 aThe percentage CO2 loss of liquid inlet is calculated as the molar flow of liquid CO2 leav-ing the column divided by the kg CO2 fed to the column divided by the molar mass of CO2 (i.e.
44 g/mole) and multiplied by 100.
bThe percentage CO2 loss of total CO2 amount is calculated as the molar flow of liquid CO2 leaving the column divided by the sum of the gas and liquid inlet (kg liquid CO2 divided by 44 kmole gas) and multiplied by 100.
The percentage The feed stream f was fed at the bottom of the purification col-umn Al at a flow of approximately 100 kmole/hour. The major compo-nent was carbon dioxide contaminated with minor amounts of the com-ponents as indicated in the table.
The liquid absorbent carbon dioxide stream 10 was fed at the top of the purification column at different flow rates in the range 400 - 2000 kg/hour as indicated in the table above.
The contaminant rich liquid 12 left the purification column at the bottom section and was discarded or re-boiled according to the prior art method and fed to the gaseous feed stream again and fed to the purifi-cation column.
The contaminant lean carbon dioxide enriched stream leaving the column at the top section was stored or further processed before be-ing stored, e.g. by filtration and distillation.
From the table it is evident that under the above conditions the lowest applicable flow rate of liquid carbon dioxide was approximately 400 kg/hour. At this flow rate only n-propane was completely reduced;
toluene, methanol, ethanol and iso-butanol to over 99%.
Increasing flow rates increased the number of components that were washed out. Thus, depending on the composition of the feed gas the flow rate must be adjusted for optimal results. In the top row the amount of carbon dioxide waste is illustrated. Thus, it can be seen that increasing the flow of liquid carbon dioxide effectuated a more efficient washing out of contaminants, however the amount of waste carbon diox-ide in the contaminant rich stream increased dramatically from 1.53% at 500 kg/hour to 24.41 % at 2000 kg/hour. Though not shown, increasing the amount of liquid carbon dioxide above 2000 kg/hour would result in even higher percentages of carbon dioxide in the contaminant rich frac-tion.
Recirculating this contaminant rich carbon dioxide by means of a reboiler as suggested in the prior art would require a large energy in-put as outlined in table 3 below.

Example 1 A feed stream was treated according to the method described in the comparative example. In addition a blower, i.e. compressing means, was inserted in accordance with alternative 1 according to the present 5 invention.
Table 2 Pressure in column bar 22.8 Absorbent liquid carbon dioxide fed to column (kg/hour) 12,000 10,500 9000 7500 6000 4500 3000 1500 Flowrates in feed gas kmole/hour % Recovery to liquid outlet Nitrogen 0.01 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Oxygen 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 Methane 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.01 0.02 Carbon Dioxide 100.00 0.67 0.74 0.82 0.92 1.05 1.23 1.46 1.76 -Hydrogen Sulfide 0.01 1.53 1.62 1.72 1.85 2.00 2.20 2.52 2.98 Carbonyl Sulfide 0.01 89.39 89.03 88.37 87.43 85.16 80.73 70.44 42.99 Dimethyl Ether 0.01 99.95 99.95 99.94 99.91 99.91 99.86 99.72 98.81 N-Pentane 0.01 99.97 99.97 99.96 99.94 99.94 99.92 99.83 99.30 -Nitrogen Dioxide 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 N-Hexane 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Acetaldehyde 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Ethyl Acetate 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Dimeth (Sulfide 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Benzene 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Acetone 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Toluene 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Methanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Ethanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Isobutanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 N-Propanol 0.01 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 Feed gas temp C 10.70 Gas Outlet temp C -19.0 -19.0 -19.0 -19.0 -19.0 -19.0 -19.0 -19.0 -Liquid Feed temp. C -18.20 -22.0 -22.0 -22.0 -22.0 -22.0 -22.0 -22.0 -22.0 Liquid outlet temp. C 18.74 -18.75 -18.57 -17.66 -16.28 5.24 From table 2 it can be seen that the amount of carbon dioxide in the overall process was substantially reduced as compared to the com-10 parative example for which the results are shown in table 1. Thus, the waste liquid (13) comprised only minor volumes of carbon dioxide.
The energy consumption that would be required by the prior art method and the method of the present invention respectively has been compared.
15 In a recovery unit of the size illustrated, i.e. processing 100 kmole feed gas per hour, approximately 30 kWh internal energy is avail-able ("internal energy" means energy that is neutral to the refrigeration load). The internal energy available will increase with the size of the unit.
In table 3 below the energy consumption is analysed. In a plant operating at 100 kmole feed stream/hour the internal heat available typically corresponds to 30 kWh. "Additional power prior art" in table 3 is the extra power required in order to reduce the CO2 loss to the same level as for the present invention. Heat required above this value must be supplied from external sources.

Table 3 Absorbent liquid carbon dioxide 12,000 10,500 9,000 7,500 6,000 4,500 3,000 1,500 (kg/hour) 881.2 765.3 649.5 533.6 417.7 301.8 186.0 70.4 Reboiler duty (kWh) Additional power prior art (kWh) 425.61 3676.7 309.73 251.78 193.84 135.90 78.00 20.22 Additional power 12.3 10.7 9.0 7.4 5.8 4.2 2.6 1.0 for refrigeration (kWh) Additional power for blower 24.5 21.3 18.1 14.9 11.6 8.4 5.2 2.0 (kWh) Total additional power present 36.8 32.0 27.1 22.3 17.5 12.6 7.8 3.0 invention (kWh) From the table it is clearly seen that when applying the solution provided by the present invention the overall energy needed for providing a clean product stream without compromising the yield of carbon dioxide is markedly reduced.

Claims

1. A method for removing at least one contaminant from a feed stream (f) substantially comprising carbon dioxide, said method com-prising the step of subjecting the feed stream (f) to a) a purification step in a column having a top, bottom and an Intermediate section, the purification step provides a contaminant lean stream (g2) leaving the top section of the column and a contaminant rich liquid stream (12) leaving, optionally the bottom section of, the col-umn, said contaminant rich liquid stream (12) being fed to the reboiler (A3) and wherein the contaminant lean stream leaving the top section of the column is further subjected to the steps selected from the two op-tions:
1:
b1) compressing the contaminant lean stream (g2) providing a compressed gaseous stream (g4) c1) cooling the compressed gaseous stream (g4) in the reboiler (A3) providing at least a product stream (p) and a gaseous stream (g3);
and d1) feeding the gaseous stream (g3) to the column at the bot-tom section of the column;
and

2:
b2) cooling the contaminant lean stream (g2) in a reboiler pro-viding at least a product stream (p) and a gaseous stream (g3); and c2) compressing the gaseous stream (g3) providing a cooled compressed gaseous stream (g4');
d2) feeding the cooled compressed gaseous stream (g4') to the column at the bottom section of the column; and depressurising the con-taminant rich liquid stream (12) leaving at the bottom section of the col-umn before entering the reboiler;
wherein the purification step is selected from absorption using an absorbent when the feed stream is gaseous, and rectification having a liquid phase, when the feed stream is liquid, and wherein the absor-bent and liquid phase is liquid carbon dioxide.

2. The method according to claim 1, wherein the feed stream is liquid and the further steps are:
b1) compressing the contaminant lean stream (g2) providing a compressed gaseous stream (g4) c1) cooling the compressed gaseous stream (g4) in a reboiler providing at least a product stream (p) and a gaseous stream (g3); and d1) feeding the gaseous stream (g3) to the column at the bot-tom section of the column,

3. The method according to claim 1 , wherein the feed stream (f) is gaseous.

4. The method according to claim 3, wherein the further steps are:
b2) cooling the contaminant lean stream (g2) in a reboiler pro-viding at least a product stream (p) and a gaseous stream (g3); and c2) compressing the gaseous stream (g3) providing a cooled compressed gaseous stream (g4');
d2) feeding the cooled compressed gaseous stream (g4') to the column at the bottom section of the column; and depressurising the con-taminant rich liquid stream (12) leaving at the bottom section of the col-umn before entering the reboiler.

5. The method according to any of the preceding claims wherein the at least one contaminant is selected among compounds having a boiling point higher than the boiling point of carbon dioxide at the pre-vailing conditions and non-polar compounds.

6. The method according to claim 5, wherein the at least one contaminant is selected from the group consisting of: sulfides, such as hydrogen sulfide, carbonyl sulfides and dimethylsulfide; nitrogen con-taining compounds, such as N2, ammonia and nitrogen dioxide; and hy-drocarbons, such as, methane, n-pentane, n-hexane, benzene, toluene and oxygen containing hydrocarbons such as dimethyl ether, acetalde-hyde, ethyl acetate, acetone, methanol, ethanol, isobutanol and n-propanol.

7. The method according to any of the preceding claims, wherein ratio of liquid carbon dioxide to the feed stream is 1:3 to 10:1, preferably 1:3 to 3:1.

8. The method according to any of the preceding claims, wherein the purification step further comprises an integrated water in-hibitor and/or scavenger step.

9. The method according to claim 8, wherein the water inhibitor and/or scavenger used In the purification step is recirculated in the proc-ess.

10. The method according to any of the claims 8 or 9, wherein the water inhibitor and/or scavenger is fed to the intermediate section of the purification column.

11. The method according to any of the claims 9 or 10 wherein the water inhibitor and/or scavenger is mixed with the feed stream (f) or the absorbent liquid (I1) prior to being fed to the column.

12. The method according to any of the claims 8-11, wherein a liquid carbon dioxide stream (15) is partially withdrawn from the purifica-tion column at a position above the inlet of the water inhibitor and/or scavenger.

13. The method according to any of the claims 8 to 12, wherein the integrated inhibitor step is a dehydration step using a water inhibi-tor, which decreases the water activity in the feed stream, such as methanol, ethanol, mono ethylene glycol and tri ethylene glycol.

14. The method according to any of the preceding claims further comprising at least one of the steps of:
- heating or cooling the product stream leaving the reboiler, and/or - purifying the product stream by means of adsorption and/or absorption; and/or - condensing and/or distilling the product stream to provide a high purity liquid carbon dioxide stream; and/or - feeding a portion of condensed and/or refluxed carbon diox-ide to the purification column.

15. The method according to any of the preceding claims wherein the purification step is preceded by at least one or more of the steps of:
- compressing, - adsorbing and/or absorbing; and - liquefying by means of for example condensation or distilla-tion,

16. A carbon dioxide purification unit comprising a purification column (A1), a compression means (A2), and a reboiler (A3), said purifi-cation column (A1) having a top and a bottom and a section intermedi-ate of the top and the bottom, the purification column having a feeding stream influent (f), a contaminant lean gas effluent (g2) situated at the top part of the column, a liquid carbon dioxide influent (11) situated at the top part of the column, and a contaminant rich liquid effluent (12), said contaminant rich liquid effluent (12) optionally being situated at the bottom part of the purification column, wherein the contaminant rich liquid effluent (12) is connected to the reboiler (A3) additionally having a waste liquid effluent (13), a prod-uct effluent (p), a compressed gaseous influent (g4), and a gas effluent (g3), the gaseous effluent (g3) being connected to the purification col-umn (A1), wherein the compressing means (A2) is inserted between the reboiler (A3) and the purification column (A1) at a position where the contaminant lean gas purification column effluent (g2) is compressed to provide the compressed gaseous influent (g4);
or wherein the contaminant rich liquid effluent (12) is connected to the reboiler (A3) additionally having a waste liquid effluent (13), a prod-uct effluent (p), a contaminant lean gas purification column effluent (g2), and a gas effluent (g3), the gas effluent (g3) being connected to the compressing, means (A2) inserted between the reboiler (A3) and the purification column (A1) at a position between the gas effluent (g3) and a cooled compressed gaseous influent (g4') connected to the column (A1) and wherein the unit further comprises a depressurising valve (A4), wherein the depressurising valve (A4) is positioned on the contaminant rich liquid effluent (12).

17. The unit according to claim 16, wherein the feeding influent (f) is situated at the bottom section of the purification column (A1) and the contaminant rich liquid effluent (12) is connected to the reboiler (A3) additionally having a waste liquid effluent (13), a product effluent (p), a compressed gaseous influent (g4), and a gas effluent (g3), the gas ef-fluent (g3) being connected to the purification column (A1), wherein a compressing means (A2) is inserted between the reboiler (A3) and the purification column (A1) at a position between the contaminant lean gas purification column effluent (g2) and the compressed gaseous influent (g4) and wherein the purification column is an absorption column.

18. The unit according to claim 16, wherein the feeding Influent (f) is situated at the top section of the purification column (A1) and the contaminant rich liquid effluent (12) is connected to the reboiler (A3) ad-ditionally having a waste liquid effluent (13), a product effluent (p), a contaminant lean gas purification column effluent (g2), and a gas efflu-ent (g3), the gas effluent (g3) being connected to a compressing means (AZ) inserted between the reboiler (A3) and the purification column (A1) at a position between the gas effluent (g3) and the cooled compressed gaseous influent (g4') and wherein a valve (A4) is positioned on the con-taminant rich liquid effluent (12) and wherein the purification column is a rectification column.

19 The unit according to any of the claims 16 to 18, wherein the purification column further comprises a water inhibitor and/or scavenger influent (10) situated at the intermediate section of the column.

20. The unit according to any of the claims 6 to 19, wherein the contaminant rich liquid effluent (12) situated at the bottom section of the column is split in two at a position outside the column and a first liq-uid effluent (12') is connected to the water inhibitor and/or scavenger in-fluent (10) and a second liquid effluent (12") is connected to the reboiler (A3).

21. The unit according to any of the claims 19 to 20, wherein the purification column Is further provided with a carbon dioxide effluent (IS) situated at a position of the purification column between the water inhibitor and/or scavenger influent (10) and the liquid carbon dioxide in-fluent (11).

22. The unit according to any of the claims 16 to 21, wherein the unit further comprises a feeding gas source, and wherein the feeding influent (f) is connected to the feeding gas source, preferably partially purified carbon dioxide; and/or Wherein the unit further comprises a carbon dioxide processing unit such as a heat exchanger and/or a filter and/or a distillation column, and wherein the product effluent (p) is connected to the carbon dioxide processing unit,; and/or wherein the unit further comprises a liquid carbon dioxide res-ervoir, e.g, a distillation column connected to the product gas outlet and wherein the liquid carbon dioxide influent (11) is connected to the liquid carbon dioxide reservoir,; and/or wherein the unit further comprises a waste reservoir, and wherein the waste liquid effluent (13) is connected to the waste reser-voir; and/or wherein the unit further comprises a water inhibitor/scavenger reservoir and wherein the water inhibitor and/or scavenger influent (10) is connected to the water inhibitor/scavenger reservoir.

23. The unit according to any of the claims 16 to 22, further comprising a drying filter, and a compressor wherein the feeding influent (f) up stream is connected to the drying filter, which optional drying fil-ter is connected to the compressor.

24. The unit according to any of the claims 21 to 23 wherein the carbon dioxide effluent (15) is connected to the feeding influent (f).